CN102875317A - Method for producing p-xylene - Google Patents
Method for producing p-xylene Download PDFInfo
- Publication number
- CN102875317A CN102875317A CN2011101934255A CN201110193425A CN102875317A CN 102875317 A CN102875317 A CN 102875317A CN 2011101934255 A CN2011101934255 A CN 2011101934255A CN 201110193425 A CN201110193425 A CN 201110193425A CN 102875317 A CN102875317 A CN 102875317A
- Authority
- CN
- China
- Prior art keywords
- xylol
- distribution pipe
- main reaction
- catalyst
- reaction region
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method for producing p-xylene, mainly solving the problem of low yield of p-xylene in the prior art. The method disclosed herein mainly comprises the following steps: letting a raw material containing toluene enter into a mixing contact zone to contact with a catalyst and a methanol raw material which enters into the mixing contact zone through a distribution pipe, letting the formed gas-phase flow enter a main reaction zone above the distribution pipe to generate a product flow of p-xylene and simultaneously form a regeneration catalyst; (2) letting the regeneration catalyst enter into a regenerator for regenerating to form a regenerated catalyst; and (c) letting the regenerated catalyst return to the main reaction zone, wherein the regenerator is a riser. The method disclosed herein well solves the problems and can be used in the industrial production of p-xylene.
Description
Technical field
The present invention relates to a kind of method of producing p-Xylol, be particularly useful for being prepared by methyl alcohol and toluene the method for p-Xylol.
Background technology
Dimethylbenzene is important basic raw material, especially p-Xylol.P-Xylol is the basic raw material of synthesizing polyester (PET), and toluene, C are mainly adopted at present p-Xylol production
9Aromatic hydrocarbons and xylol are raw material, prepare by disproportionation, isomerization, fractionation by adsorption or low temperature separation process.Because the p-Xylol content in its product is subjected to thermodynamic control, p-Xylol is at C
8Only account for approximately 24% in the BTX aromatics, solid circulating rate is very large in the technological process, and process cost is higher.In recent years, the lot of domestic and international patent disclosure preparation p-Xylol a lot of variation routes, wherein, paid much attention to by the technology that methylation reaction prepares p-Xylol by methyl alcohol and toluene.Because the boiling point of three isomer differs very little in the dimethylbenzene, by the highly purified p-Xylol of the very difficult acquisition of the distillation technique of routine.The selectivity of the raising p-Xylol that therefore need in the process of preparation dimethylbenzene, try one's best.
After nineteen seventies ZSM-5 synthesizes successfully, because this catalyzer all has unique catalytic performance to many reactions such as alkylation, isomerization, phenyl ring methylate, cause extensive attention.The pore canal system that ZSM-5 zeolite is made of 10 yuan of rings, have medium sized aperture and aperture, can allow molecular diameter is that the p-Xylol of 0.63 nanometer spreads rapidly, can effectively hinder o-Xylol, m-xylene diffusion that molecular diameter is 0.69 nanometer simultaneously.This fact means carries out the possibility that shape is selected to toluene phenyl ring methylation reaction, can obtain to be higher than in the dimethylbenzene product p-Xylol content of thermodynamic(al)equilibrium concentration far away.
CN1326430 discloses the method that a kind of alkylated aromatic hydrocarbons reactant is produced alkylation aromatic products, and especially for the methanol toluene methylation reaction, its feature mainly is to have adopted the method that toluene, methyl alcohol are introduced reactor in different positions to prepare dimethylbenzene.CN1355779 discloses a kind of method of direct selective synthesis of para-xylene, the aromatic hydroxy compound by will comprising toluene, benzene and composition thereof with by CO, CO
2, H
2And composition thereof the methylating reagent reaction that forms, the method makes at least 5% aromatic hydroxy compound be converted into xylene mixture, wherein p-Xylol accounts at least 30% of xylene mixture.
CN1231653 discloses the method that a kind of selectivity is made p-Xylol, and on the catalyzer that a kind of porous crystalline material is made, this catalyzer comprises the oxide compound that ZSM-5 or ZSM-11 zeolite and modification use, with methyl alcohol and toluene reaction preparation p-Xylol.CN1775715 discloses a kind of method for preparing the dimethylbenzene product, uses a kind of ZSM-5 zeolite ability catalyzer of phosphorous modification, toluene, methyl alcohol, hydrogen are introduced reactor, but the toluene conversion in the method is on the low side, and the highest only have 23%.CN1759081 discloses a kind of method for preparing p-Xylol, adopt the ZSM-5 zeolite catalyzer of oxide modifying, in flow reactor, under high linear speed, operate, reactant and catalyzer duration of contact were less than 1 second, can improve Selectivity for paraxylene, but the toluene conversion of the method is on the low side, the highest only have 22%.
All there is the lower problem of dimethylbenzene yield in prior art, and the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the low problem of the p-Xylol yield that exists in the prior art, and a kind of method of new production p-Xylol is provided.The method is used for the production of p-Xylol, has the higher advantage of p-Xylol yield.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of method of producing p-Xylol, mainly may further comprise the steps: (1) comprises that the raw material of toluene enters mixing contact area from grid distributor, contact with the methanol feedstock that enters mixing contact area from distribution pipe with catalyzer, the gaseous stream that forms enters the main reaction region of distribution pipe top, generation comprises the product stream of p-Xylol, forms simultaneously reclaimable catalyst; (2) described reclaimable catalyst enters revivifier regeneration, forms regenerated catalyst; (3) described regenerated catalyst returns main reaction region; Wherein, revivifier is riser tube.
In the technique scheme, described mixing contact area and main reaction region are fluidized-bed, and catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200; The grid distributor percentage of open area is 0.55～0.75, and distribution pipe is dendritic, and the pneumatic outlet direction deflection on the distribution pipe is lower; The average carbon deposition quantity massfraction of reclaimable catalyst is 0.4～1.8%, and the average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; The temperature of reaction of described main reaction region is 350～500 ℃, and reaction pressure is counted 0.01～2.0MPa with gauge pressure, and the gas phase linear speed is 0.3～1.5 meter per second; Described methanol feeding temperature is 60～200 ℃, and methyl alcohol is first through entering distribution pipe behind the heat production coil pipe that is arranged at main reaction region inside again; Described reclaimable catalyst is regenerated through entering revivifier behind the water vapour stripping in stripper; The charging mass ratio of described toluene and methyl alcohol is 10～1: 1.
The method of calculation of average coke content of the present invention are that carbon deposit quality on the catalyzer is divided by described catalyst quality.Carbon deposit measuring method on the catalyzer is as follows: will mix comparatively uniform catalyst mix with carbon deposit, then the band C catalyst of weighing 0.1～1 gram, be put in the pyrocarbon analyser and burn, the carbonic acid gas quality that generates by infrared analysis burning, thus carbonaceous amount on the catalyzer obtained.
Toluene conversion of the present invention, methanol conversion, dimethylbenzene selective, Selectivity for paraxylene method of calculation are:
Toluene conversion, the toluene quality in the %=100-product/methylbenzene raw material quality * 100%;
Methanol conversion, the methanol quality in the %=100-product/methanol feedstock quality * 100%;
Dimethylbenzene selective, the quality of dimethylbenzene/methylbenzene raw material quality * 100% in the %=product;
Selectivity for paraxylene, the quality of dimethylbenzene * 100% in the quality/product of p-Xylol in the %=product.
ZSM-5 catalyzer of the present invention is take ZSM-5 molecular sieve as active main body, adopts the adding binding agent to prepare by the method for spraying drying, roasting moulding.The binding agent that adds can make SiO
2Or Al
2O
3, the add-on of binding agent is counted between 10～80% with its per-cent in moulding rear catalyst quality.The catalyzer of moulding for example adopts the polysiloxane of phenyl methyl polysiloxane to select the shape processing.
Among the present invention, percentage of open area refers to the useful area of grid distributor, namely refers to the area summation in hole on the grid distributor face and the ratio of the grid distributor face total area.
The inventor finds that by research the ratio by toluene and methyl alcohol in the increase feed zone will effectively reduce the side reaction that methyl alcohol causes, and improve the yield of dimethylbenzene.Adopt method of the present invention, mixing contact area is set, toluene enters mixing contact area from the grid distributor of mixing contact area bottom, methyl alcohol enters mixing contact area from the distribution pipe at mixing contact area top, be the counter current contact method, effectively realized the well blend of toluene, methyl alcohol, catalyzer, and guarantee that it is the toluene environment that methyl alcohol enters what contact after the mixing contact area, control simultaneously the methanol feeding temperature, the occurrence probability that to greatly reduce methanol conversion be low-carbon alkene, be decomposed into the side reactions such as CO and H2 has improved the yield of dimethylbenzene.In addition, because the coking yield of methylbenzene methanol methylation reaction is lower on the ZSM-5 catalyzer, revivifier adopts riser tube rapid regeneration mode, has effectively guaranteed the catalyst activity in the main reaction region.Also have, methyl alcohol first through being arranged at the sampling coil pipe of main reaction region inside, and enters mixing contact area through distribution pipe behind the media for heat exchange in the main reaction region again before entering mixing contact area, has realized the effect of heat-obtaining and pre-hot methanol in the main reaction region.Therefore, adopt method of the present invention, be provided with mixing contact area, adopt the toluene feeding manner different with methyl alcohol, Effective Raise the yield of dimethylbenzene.
Adopt technical scheme of the present invention: described mixing contact area and main reaction region are fluidized-bed, and catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200; The grid distributor percentage of open area is 0.55～0.75, and distribution pipe is dendritic, and the pneumatic outlet direction deflection on the distribution pipe is lower; The average carbon deposition quantity massfraction of reclaimable catalyst is 0.4～1.8%, and the average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; The temperature of reaction of described main reaction region is 350～500 ℃, and reaction pressure is counted 0.01～2.0MPa with gauge pressure, and the gas phase linear speed is 0.3～1.5 meter per second; Described methanol feeding temperature is 60～200 ℃, and methyl alcohol is first through entering distribution pipe behind the heat production coil pipe that is arranged at main reaction region inside again; Described reclaimable catalyst is regenerated through entering revivifier behind the water vapour stripping in stripper; The charging mass ratio of described toluene and methyl alcohol is 10～1: 1, toluene conversion reaches more than 35%, and methanol conversion reaches more than 99%, and Selectivity for paraxylene reaches more than 98%, p-Xylol once through yield based on toluene reaches more than 34%, has obtained preferably technique effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is the toluene feed grid distributor; 2 is the toluene feed pipeline; 3 is the methanol feeding distribution pipe; 4 is mixing contact area; 5 is methanol feed line; 6 is regenerator sloped tube; 7 is settling vessel; 8 is cyclonic separator; 9 is the product gas outlet pipeline; 10 is collection chamber; 11 is main reaction region; 12 is revivifier; 13 is degassed medium feeding line; 14 is the regeneration air feed pipeline; 15 is degas zone; 16 is the revivifier settling vessel; 17 slightly revolve for leg outlet; 18 is cyclonic separator; 19 is exhanst gas outlet; 20 is the raising section; 21 is inclined tube to be generated; 22 is the stripped vapor feeding line; 23 is stripper.
The raw material that comprises toluene enters mixing contact area 4 from grid distributor 1, contact with the methanol feedstock that enters mixing contact area 4 from distribution pipe 3 with catalyzer, the main reaction region 11 that the gaseous stream that forms enters distribution pipe 3 tops, generation comprises the product stream of p-Xylol, form simultaneously reclaimable catalyst, reclaimable catalyst enters stripper 23, through entering revivifier 12 regeneration behind the stripping, form regenerated catalyst, regenerated catalyst returns main reaction region 11 through degas zone 15 is degassed by regenerator sloped tube 6.
The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.
Embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 200, and the binding agent mass content is 45% in the catalyzer, and binding agent is SiO
2The ZSM-5 molecular sieve mass content is 45%, methylbenzene raw material enters mixing contact area from grid distributor, contact with the methanol feedstock that enters mixing contact area from distribution pipe with catalyzer, the gaseous stream of formation enters the main reaction region of distribution pipe top, generates the product stream that comprises p-Xylol, form simultaneously reclaimable catalyst, reclaimable catalyst enters revivifier regeneration, forms regenerated catalyst, and regenerated catalyst returns main reaction region.Revivifier is riser tube, mixing contact area and main reaction region are fluidized-bed, the grid distributor percentage of open area is 0.55, distribution pipe is dendritic, pneumatic outlet direction deflection on the distribution pipe is lower, with the horizontal direction angle be 48 the degree, the average carbon deposition quantity massfraction of reclaimable catalyst is 0.4%, the average carbon deposition quantity massfraction of regenerated catalyst is 0.01%, the temperature of reaction of main reaction region is 350 ℃, reaction pressure is counted 0.01MPa with gauge pressure, the gas phase linear speed is 0.3 meter per second, and the methanol feeding temperature is 60 ℃, and methyl alcohol is first through entering distribution pipe behind the heat production coil pipe that is arranged at main reaction region inside again, through entering revivifier regeneration behind the water vapour stripping, the charging mass ratio of toluene and methyl alcohol is 10: 1 to reclaimable catalyst in stripper.The liquid phase product is by gas chromatographic analysis, and analytical results is: toluene conversion is 27.96%, and methanol conversion is 97.14%, and dimethylbenzene selective is 73.28%, and Selectivity for paraxylene is 90.33%.
[embodiment 2]
According to embodiment 1 described condition and step, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20, the grid distributor percentage of open area is 0.75, the average carbon deposition quantity massfraction of reclaimable catalyst is 1.8%, the average carbon deposition quantity massfraction of regenerated catalyst is 0.5%, the temperature of reaction of main reaction region is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 1.5 meter per seconds, the methanol feeding temperature is 200 ℃, and the charging mass ratio of toluene and methyl alcohol is 1: 1.The liquid phase product is by gas chromatographic analysis, and analytical results is: toluene conversion is 35.22%, and methanol conversion is 99.23%, and dimethylbenzene selective is 87.25%, and Selectivity for paraxylene is 95.27%.
[embodiment 3]
According to embodiment 1 described condition and step, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 50, the grid distributor percentage of open area is 0.7, the average carbon deposition quantity massfraction of reclaimable catalyst is 1.5%, the average carbon deposition quantity massfraction of regenerated catalyst is 0.15%, the temperature of reaction of main reaction region is 450 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 0.7 meter per second, the methanol feeding temperature is 130 ℃, and the charging mass ratio of toluene and methyl alcohol is 2: 1.The liquid phase product is by gas chromatographic analysis, and analytical results is: toluene conversion is 35.09%, and methanol conversion is 98.67%, and dimethylbenzene selective is 89.36%, and Selectivity for paraxylene is 98.14%.
[embodiment 4]
According to embodiment 3 described condition and steps, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 100, the grid distributor percentage of open area is 0.75, the average carbon deposition quantity massfraction of reclaimable catalyst is 1.2%, the average carbon deposition quantity massfraction of regenerated catalyst is 0.1%, the temperature of reaction of main reaction region is 430 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 0.5 meter per second, the methanol feeding temperature is 100 ℃, and the charging mass ratio of toluene and methyl alcohol is 3: 1.The liquid phase product is by gas chromatographic analysis, and analytical results is: toluene conversion is 33.43%, and methanol conversion is 95.11%, and dimethylbenzene selective is 84.19%, and Selectivity for paraxylene is 93.16%.
[embodiment 5]
According to embodiment 4 described condition and steps, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 80, the grid distributor percentage of open area is 0.75, the average carbon deposition quantity massfraction of reclaimable catalyst is 1.25%, the average carbon deposition quantity massfraction of regenerated catalyst is 0.12%, the temperature of reaction of main reaction region is 463 ℃, and reaction pressure is counted 2.0MPa with gauge pressure, and the gas phase linear speed is 0.43 meter per second, the methanol feeding temperature is 180 ℃, and the charging mass ratio of toluene and methyl alcohol is 2: 1.The liquid phase product is by gas chromatographic analysis, and analytical results is: toluene conversion is 31.76%, and methanol conversion is 94.02%, and dimethylbenzene selective is 92.11%, and Selectivity for paraxylene is 89.24%.
[comparative example 1]
According to embodiment 3 described condition and steps, mixing contact area is not set, whole methyl alcohol and toluene enter main reaction region from the main reaction region bottom together, analytical results is: toluene conversion is 33.34%, methanol conversion is 96.13%, dimethylbenzene selective is 82.46%, and Selectivity for paraxylene is 93.45%.
Obviously, adopt method of the present invention, can reach the purpose that improves the p-Xylol yield, have larger technical superiority, can be used in the industrial production of dimethylbenzene.
Claims (8)
1. method of producing p-Xylol mainly may further comprise the steps:
(1) raw material that comprises toluene enters mixing contact area from grid distributor, contact with the methanol feedstock that enters mixing contact area from distribution pipe with catalyzer, the gaseous stream that forms enters the main reaction region of distribution pipe top, generates the product stream that comprises p-Xylol, forms simultaneously reclaimable catalyst;
(2) described reclaimable catalyst enters revivifier regeneration, forms regenerated catalyst;
(3) described regenerated catalyst returns main reaction region;
Wherein, revivifier is riser tube.
2. the method for described production p-Xylol according to claim 1 is characterized in that described mixing contact area and main reaction region are fluidized-bed, and catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200.
3. the method for described production p-Xylol according to claim 1 is characterized in that described grid distributor percentage of open area is 0.55～0.75, and distribution pipe is dendritic, and the pneumatic outlet direction deflection on the distribution pipe is lower.
4. the method for described production p-Xylol according to claim 1 is characterized in that the average carbon deposition quantity massfraction of described reclaimable catalyst is 0.4～1.8%, and the average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%.
5. the method for described production p-Xylol according to claim 1 is characterized in that the temperature of reaction of described main reaction region is 350～500 ℃, and reaction pressure is counted 0.01～2.0MPa with gauge pressure, and the gas phase linear speed is 0.3～1.5 meter per second.
6. the method for described production p-Xylol according to claim 1 is characterized in that described methanol feeding temperature is 60～200 ℃, and methyl alcohol is first through entering distribution pipe behind the heat production coil pipe that is arranged at main reaction region inside again.
7. the method for described production p-Xylol according to claim 1, it is characterized in that described reclaimable catalyst in stripper through entering revivifier regeneration behind the water vapour stripping.
8. the method for described production p-Xylol according to claim 1, the charging mass ratio that it is characterized in that described toluene and methyl alcohol is 10～1: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193425.5A CN102875317B (en) | 2011-07-12 | 2011-07-12 | Method for producing p-xylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193425.5A CN102875317B (en) | 2011-07-12 | 2011-07-12 | Method for producing p-xylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102875317A true CN102875317A (en) | 2013-01-16 |
| CN102875317B CN102875317B (en) | 2014-11-26 |
Family
ID=47476879
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110193425.5A Active CN102875317B (en) | 2011-07-12 | 2011-07-12 | Method for producing p-xylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102875317B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018118595A1 (en) * | 2016-12-20 | 2018-06-28 | Uop Llc | Processes and apparatuses for toluene methylation in an aromatics complex |
| WO2018118675A1 (en) * | 2016-12-20 | 2018-06-28 | Uop Llc | Processes and apparatuses for toluene methylation in an aromatics complex |
| KR20190140468A (en) * | 2017-04-27 | 2019-12-19 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the preparation of paraxylene with methanol and / or dimethylether and benzene and the simultaneous production of low carbon olefins |
| JP2020517589A (en) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Fluidized bed apparatus and method for producing para-xylene from methanol and/or dimethyl ether and toluene and co-producing lower olefins |
| CN112313193A (en) * | 2018-06-25 | 2021-02-02 | 沙特基础工业全球技术有限公司 | Method and system for producing paraxylene |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1898185A (en) * | 2003-09-30 | 2007-01-17 | 沙地基本工业公司 | Toluene methylation process |
| CN101333140A (en) * | 2008-07-08 | 2008-12-31 | 中国石油化工股份有限公司 | Reaction device for preparing low carbon olefin from methanol or dimethyl ether |
| CN101417236A (en) * | 2007-10-24 | 2009-04-29 | 中国科学院大连化学物理研究所 | Movable bed catalyst for alkylation of toluene and methanol to produce paraxylene and low-carbon olefin |
| CN101456784A (en) * | 2007-12-12 | 2009-06-17 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing light olefins by toluene and methylating reagent |
-
2011
- 2011-07-12 CN CN201110193425.5A patent/CN102875317B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1898185A (en) * | 2003-09-30 | 2007-01-17 | 沙地基本工业公司 | Toluene methylation process |
| CN101417236A (en) * | 2007-10-24 | 2009-04-29 | 中国科学院大连化学物理研究所 | Movable bed catalyst for alkylation of toluene and methanol to produce paraxylene and low-carbon olefin |
| CN101456784A (en) * | 2007-12-12 | 2009-06-17 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing light olefins by toluene and methylating reagent |
| CN101333140A (en) * | 2008-07-08 | 2008-12-31 | 中国石油化工股份有限公司 | Reaction device for preparing low carbon olefin from methanol or dimethyl ether |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018118595A1 (en) * | 2016-12-20 | 2018-06-28 | Uop Llc | Processes and apparatuses for toluene methylation in an aromatics complex |
| WO2018118675A1 (en) * | 2016-12-20 | 2018-06-28 | Uop Llc | Processes and apparatuses for toluene methylation in an aromatics complex |
| KR20190140468A (en) * | 2017-04-27 | 2019-12-19 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the preparation of paraxylene with methanol and / or dimethylether and benzene and the simultaneous production of low carbon olefins |
| JP2020517596A (en) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Fluidized bed apparatus and method for producing para-xylene from methanol and/or dimehil ether and benzene and co-producing lower olefins |
| JP2020517589A (en) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Fluidized bed apparatus and method for producing para-xylene from methanol and/or dimethyl ether and toluene and co-producing lower olefins |
| KR102309236B1 (en) | 2017-04-27 | 2021-10-06 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the simultaneous production of low-carbon olefins and the production of para-xylene with methanol and/or dimethyl ether and benzene |
| US11161085B2 (en) | 2017-04-27 | 2021-11-02 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Fluidized bed device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene |
| CN112313193A (en) * | 2018-06-25 | 2021-02-02 | 沙特基础工业全球技术有限公司 | Method and system for producing paraxylene |
| CN112313193B (en) * | 2018-06-25 | 2023-10-31 | 沙特基础工业全球技术有限公司 | Method and system for producing para-xylene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102875317B (en) | 2014-11-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102463086B (en) | Reaction device for co-producing low-carbon olefin and p-xylene | |
| CN102464557B (en) | Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene | |
| CN101165017B (en) | Production increasing method for propylene | |
| KR102309241B1 (en) | Apparatus and method for simultaneous production of para-xylene and low-carbon olefin using methanol and/or dimethyl ether and toluene | |
| CN102463084B (en) | Reaction device for preparing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| US11180431B2 (en) | Fluidized bed device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene | |
| KR102309237B1 (en) | Apparatus and method for the simultaneous production of low-carbon olefins and the production of para-xylene with methanol and/or dimethyl ether and benzene | |
| CN102464550B (en) | Method for co-producing low carbon olefin and paraxylene | |
| CN102875317B (en) | Method for producing p-xylene | |
| KR102309236B1 (en) | Fluidized bed apparatus and method for the simultaneous production of low-carbon olefins and the production of para-xylene with methanol and/or dimethyl ether and benzene | |
| CN102875318B (en) | Reaction-regeneration device for producing p-xylene | |
| CN102463072B (en) | Reaction device for producing p-xylene | |
| CN102464549B (en) | Method for producing propylene and p-xylene | |
| CN105461497A (en) | Two-stage regenerating reaction device for preparing low-carbon olefins and aromatic hydrocarbon by converting methanol and/or dimethyl ether and reaction method for two-stage regenerating reaction device | |
| CN102463085B (en) | Reaction device for producing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| CN102464561B (en) | Methanol or dimethyl ether and method for preparing dimethylbenzene by using methylbenzene | |
| CN102464558B (en) | Method for producing paraxylene | |
| CN102464526A (en) | Method for producing low-carbon olefins from methanol | |
| CN102464560B (en) | Method for producing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| CN111100664A (en) | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol | |
| CN102875291B (en) | Method for producing low-carbon olefins from methanol | |
| CN103739427A (en) | Reaction device for producing low-carbon olefins from methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |